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Gas turbine power plant and method of operating the same |
| 7363764 |
Gas turbine power plant and method of operating the same
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| Patent Drawings: | |
| Inventor: |
Griffin, et al. |
| Date Issued: |
April 29, 2008 |
| Application: |
11/123,128 |
| Filed: |
May 6, 2005 |
| Inventors: |
Griffin; Timothy (Ennetbaden, CH)
Holmberg; Daniel (Norrkoping, SE)
Winkler; Dieter (Lauchringen, DE)
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| Assignee: |
ALSTOM Technology Ltd (Baden, CH) |
| Primary Examiner: |
Casaregola; L. J. |
| Assistant Examiner: |
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| Attorney Or Agent: |
Steptoe & Johnson LLP |
| U.S. Class: |
60/780; 60/39.12; 60/723; 60/783 |
| Field Of Search: |
60/39.12; 60/39.52; 60/723; 60/772; 60/777; 60/780; 60/783 |
| International Class: |
F02C 3/20 |
| U.S Patent Documents: |
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| Foreign Patent Documents: |
0 939 199; 0 953 748; 2 296 255 |
| Other References: |
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| Abstract: |
A method of operating a gas turbine power plant and gas turbine power plant are disclosed wherein hydrogen for the combusting process is produced by feeding natural gas mixed with steam through a membrane/partial oxidation reactor and converting the natural gas at least to H.sub.2 and CO. Thereby oxygen is transferred from the compressed air through the membrane of the membrane/partial oxidation reactor and the oxygen is used for the partial oxidation process of the natural gas. The process is followed by converting the syngas in a CO shift reactor and a CO shift reactor to a CO.sub.2 removal equipment to mainly hydrogen. |
| Claim: |
What is claimed is:
1. A method of operating a gas turbine power plant comprising: compressing air in at least one compressor; feeding the compressed air from the at least one compressorthrough a first side of a membrane/partial oxidation reactor; feeding the air from the first side of the membrane/partial oxidation reactor to a combustion chamber; combusting the air with hydrogen thereby producing flue gases; expanding the fluegases in a gas turbine driving at least one generator (9); feeding natural gas mixed with steam to a second side of the membrane/partial oxidation reactor and converting the natural gas at least to H.sub.2 and CO, whereby oxygen is transferred from thecompressed air through a membrane of the membrane/partial oxidation reactor and oxygen is used for partial oxidation of the natural gas; feeding resulting syngas to a CO shift reactor thereby producing H.sub.2 and converting a majority of remaining COto CO.sub.2; feeding the resulting syngas from the CO shift reactor to CO.sub.2 removal equipment thereby removing CO.sub.2; feeding the resulting syngas comprising H.sub.2 and H.sub.2O from the CO.sub.2 removal equipment at least to the combustionchamber.
2. The method of claim 1, further comprising: burning in a catalytic burner a fuel with the compressed air from the at least one compressor and feeding resulting gases from the catalytic burner to the first side of the membrane/partialoxidation reactor.
3. The method of claim 2, wherein the catalytic burner is used to burn at least one selected from the group consisting of natural gas and part of the resulting syngas comprising hydrogen from the CO.sub.2 removal equipment.
4. The method of claim 2, further comprising: burning in a catalytic burner a fuel with the compressed air from the compressor and feeding resulting gases from the catalytic burner to the first side of the membrane/partial oxidation reactorduring start up of the gas turbine power plant.
5. The method of claim 1, wherein produced syngas coming from the second side of the membrane/partial oxidation reactor is cooled using compressed air coming from the compressor in a heat exchanger before the syngas is fed to the CO shiftreactor.
6. The method of claim 1, wherein the natural gas mixed with steam is heated using compressed air coming from the first side of the membrane/partial oxidation reactor in a heat exchanger before the natural gas mixed with steam is fed to themembrane/partial oxidation reactor.
7. The method of claim 1, wherein the CO.sub.2 removed by the CO.sub.2 removal equipment is compressed and liquified.
8. The method of claim 1, further comprising: feeding the flue gases from the gas turbine to a heat recovery steam generator, thereby producing generated steam and expanding the generated steam in a steam turbine.
9. A gas turbine power plant comprising: at least one compressor; a membrane/partial oxidation reactor comprising a membrane, the membrane/partial oxidation reactor connected proximate a first end of a first side of the membrane to thecompressor; a combustion chamber connected to the membrane/partial oxidation reactor proximate a second end of the first side of the membrane; a gas turbine connected to the combustion chamber; a feed line connected to the membrane/partial oxidationreactor proximate a first end of a second side of the membrane; a CO shift reactor connected to the membrane/partial oxidation reactor proximate a second end of the second side of the membrane by a feed line; CO.sub.2 removal equipment connected to theCO shift reactor; and a feed line at least for hydrogen connected to the combustion chamber.
10. The gas turbine power plant of claim 9, wherein surfaces of the membrane on the second side are coated with catalytic material.
11. The gas turbine power plant of claim 10, wherein the membrane is coated with a catalyst material selected from the group consisting of Rh, Ru, Co, Fe, and bimetallic combinations thereof.
12. The gas turbine power plant of claim 9, further comprising: before the membrane/partial oxidation reactor a heat exchanger is arranged connecting an air path after the compressor proximate the first side of the membrane and one of the feedlines proximate the second side of the membrane.
13. The gas turbine power plant of claim 9, further comprising: after the membrane/partial oxidation reactor a heat exchanger is arranged connecting an air path after the compressor proximate the first side of the membrane and one of the feedlines proximate the second side of the membrane.
14. The gas turbine power plant of claim 9, further comprising: before the membrane/partial oxidation reactor a heat exchanger is arranged connecting an air path before the combustion chamber proximate the first side of the membrane and one ofthe feed lines proximate the second side of the membrane.
15. The gas turbine power plant of claim 9, further comprising: after the membrane/partial oxidation reactor a heat exchanger is arranged connecting an air path before the combustion chamber proximate the first side of the membrane and one ofthe feed lines proximate the second side of the membrane.
16. The gas turbine power plant of claim 9, further comprising: before the membrane/partial oxidation reactor a heat exchanger is arranged connecting an air path after the compressor and before the combustion chamber proximate the first side ofthe membrane and one of the feed lines proximate the second side of the membrane.
17. The gas turbine power plant of claim 9, further comprising: after the membrane/partial oxidation reactor a heat exchanger is arranged connecting an air path after the compressor and before the combustion chamber proximate the first side ofthe membrane and one of the feed lines proximate the second side of the membrane.
18. The gas turbine power plant of claim 9, wherein a catalytic burner is arranged before the membrane/partial oxidation reactor connected proximate the first end of the first side of the membrane and connected to the compressor.
19. A gas turbine power plant comprising: at least one compressor; a membrane/partial oxidation reactor comprising a membrane, the membrane/partial oxidation reactor connected proximate a first side of the membrane to the compressor; acombustion chamber connected to the membrane/partial oxidation reactor proximate the first side of the membrane; a gas turbine connected to the combustion chamber; a feed line connected to the membrane/partial oxidation reactor proximate a second sideof the membrane; a CO shift reactor connected to the membrane/partial oxidation reactor proximate the second side of the membrane by a feed line; CO.sub.2 removal equipment connected to the CO shift reactor; and a feed line at least for hydrogenconnected to the combustion chamber.
20. The gas turbine power plant of claim 19, wherein a side of the membrane is coated with catalytic material. |
| Description: |
FIELD OF THE INVENTION
The invention relates to a method of operating a gas turbine power plant and a gas turbine power plant.
BACKGROUND OF THE INVENTION
In the last years different projects were launched with the aim to develop emission free gas turbine based processes using semi-closed cycles with CO.sub.2/H.sub.2O mixtures as working fluid. Methods of operating such power plants are known forexample from EP-A1-0 939 199 and EP-A1-0 953 748. In these processes the fuel, usually natural gas, reacts with technically pure oxygen generated either in an external air-separation unit or internally in an integrated membrane reactor. One majordisadvantage of using air-separation units for these kind of processes is that they consume a great amount of energy, thus penalizing the efficiency and power output of the plant. From the literature it can be found that the energy demand forair-separation units is as high as 0.3 kWh/kg O.sub.2 produced. The energy consumption for separating the oxygen from the air can be decreased very much if oxygen-separating membranes are used. Also this technique has a few disadvantages, namely: metalto ceramic sealing is needed that can withstand temperatures >800.degree. C., the turbine inlet temperature (TIT) and the ceramic sealing temperature are linked, which limits the maximum TIT and thus lowers the performance of the plant and one needsto separate large amounts of air, corresponding to the total O.sub.2 required for full oxidation of fossil fuel powering the gas turbine.
SUMMARY OF THE INVENTION
The present invention relates to providing a method of operating a gas turbine power plant and a gas turbine power plant which avoid disadvantages of the prior as well as increasing the overall efficiency of the power plant.
This present invention is related to making use of so-called partial oxidation (POX) of the natural gas to syngas consisting of CO and H.sub.2. The oxygen required for this partial oxidation is provided by a ceramic, air separation membrane,thermally integrated into the process. This syngas would then be water gas shifted to produce even more hydrogen and convert the CO to CO.sub.2, and finally use the produced hydrogen as fuel in a gas turbine.
By doing this, one would overcome the temperature limit previously set by the membrane. The membrane reactor unit would be combined to both work as an oxygen transferring membrane and as a reactor for the partial oxidation. One membrane typethat can be used to separate the oxygen from the air is a so-called "Mixed Conducting Membrane" (MCM). These materials consist of complex crystalline structures, which incorporate oxygen ion vacancies (5-15%). The transport principle for oxygentransport through the membrane is adsorption on the surface followed by decomposition into ions, which are transported through the membrane by sequentially occupying oxygen ion vacancies. The ion transport is counterbalanced by a flow of electrons inthe opposite direction completing the circuit. The driving force is a difference in oxygen partial pressure between the permeate and retentate sides of the membrane. The transport process also requires high temperatures, i.e. >700.degree. C. In anembodiment of the present invention the surfaces of the permeate side of the membrane that contain the syngas are coated with catalytic material to promote the formation of synthesis gas 17.sub.1 and, in particular, hydrogen. Catalyst materials used forautothermal reforming are Rh, Ru, Co, Fe or bimetallic combinations thereof.
Optionally, prior to entering the membrane reactor, the air stream from the compressor can be lead to a catalytic burner where the air is heated by means of catalytic combustion. The fuel for the catalyst is either hydrogen or natural gas. Thereby the use of hydrogen is preferred to avoid producing CO.sub.2. The reason for using a catalytic burner is to increase the average temperature in the membrane/POX reactor thereby increasing the oxygen flux through the membrane. Also, thetemperature gradient in the reactor will be lower and thus the thermal stresses for the reactor will decrease.
Advantageously the syngas coming from the membrane/POX reactor consisting of hot steam, H.sub.2 and CO can enter a low temperature heat exchanger, where the syngas mixture is cooled down by an incoming stream of the compressed air from thecompressor. Another possibility would be to use a medium temperature heat exchanger to raise the temperature of the mixture of steam and natural gas before the mixture enters the membrane/POX reactor. This would flatten out the temperature profile inthe membrane/POX reactor and thus lower the temperature gradients in this.
After the expansion the hot flue gases of the gas turbine can be utilised in a heat recovery steam generator producing steam for the bottoming steam cycle and producing more power in a steam turbine and electricity in a generator.
BRIEFDESCRIPTION OF THE DRAWINGS
Preferred embodiments of the invention are illustrated in the accompanying drawings, in which:
FIG. 1 illustrates a gas turbine power plant according to the present invention; and
FIG. 2 illustrates the partial oxidation of the membrane/partial oxidation reactor.
The drawings show only the parts important for the invention. Same elements will be numbered in the same way in different drawings.
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS
FIG. 1 shows a syngas based low emission power plant according to the present invention. Air 1 is fed through a compressor 2 before the compressed air 3 is fed at least through a membrane/partial oxidation (POX) reactor 4. After themembrane/POX reactor 4 the air is burned in a combustion chamber 5 together with hydrogen 6. The flue gases are then expanded in a turbine 7, which is driving the compressor 2 and producing electricity in a generator 8. After the expansion the hot fluegases 9 are utilised in a heat recovery steam generator 10 producing steam for the bottoming steam cycle 11 and producing more power in a steam turbine 12 and electricity in a generator 13.
As can be seen from FIG. 1, natural gas 14 is being mixed with superheated intermediate pressure steam 15 and is then lead to the membrane/POX reactor 4. One possibility here would be to use a medium temperature beat exchanger 16 to raise thetemperature of the mixture of steam 15 and natural gas 14. This would flatten out the temperature profile in the membrane/POX reactor 4 and thus lower the temperature gradients in this. Since the temperature involved is not too high (<900.degree. C.), it might be possible to use a metal heat exchanger.
As seen in FIG. 2, in the membrane/POX reactor 4, oxygen is transferred through a membrane 18 from a first side to a second side and is partially oxidised (as well as reformed with steam) on the membrane 18 surface with the natural gas 14 by thefollowing reactions: CH.sub.4+0.5O.sub.22H.sub.2+CO+35.67 kJ/mol CH.sub.4+H.sub.2OCO+3H.sub.2-205 kJ/mol CO+H.sub.2OCO.sub.2+H.sub.2+41.15 kJ/mol
In sum, the three reactions combine to produce a mixture of H.sub.2, CO and CO.sub.2; the overall heat balance and product mixture is dictated by the amount of oxygen (and endothermic reactions) that is present. The design of the membrane/POXreactor 4 is such that the overall process is autothermal, and the membrane temperature is of ca. 800.degree. C. The membrane/POX reactor 4 would be combined to both work as an oxygen transferring membrane and as well as doing the partial oxidation. One membrane type that can be used to separate the oxygen from the air is a so-called "Mixed Conducting Membrane" (MCM). These materials consist of complex crystalline structures, which incorporate oxygen ion vacancies (5-15%). The transport principlefor oxygen transport through the membrane 18 is adsorption on the surface followed by decomposition into ions, which are transported through the membrane by sequentially occupying oxygen ion vacancies. The ion transport is counterbalanced by a flow ofelectrons in the opposite direction. The driving force is a difference in oxygen partial pressure between the permeate and retentate sides of the membrane 18. The transport process also requires high temperatures, i.e. >700.degree. C. In anembodiment of the present invention the surfaces of the permeate side of the membrane 18 (that containing the syngas 17.sub.1) is coated with catalytic material to promote the formation of synthesis gas 17.sub.1 and, in particular, hydrogen. Catalystmaterials used for autothermal reforming are Rh, Ru, Co, Fe or bimetallic combinations thereof (e.g. Co/Fe).
The syngas 17.sub.1, now consisting of hot steam, H.sub.2 and CO enters a low temperature heat exchanger 19, where the syngas 17.sub.1 mixture is cooled down by an incoming stream of the compressed air 3 from the compressor 2. Optionally, theair stream from the low temperature heat exchanger 19 can then be lead to a catalytic burner 20 where the air is heated by means of catalytic combustion. The fuel for the catalytic burner 20 is either hydrogen 21 or natural gas 14. Use of hydrogen 21is preferred to avoid producing CO.sub.2. The reason for using a catalytic burner 20 is to increase the average temperature in the membrane/POX reactor 4, increasing the oxygen flux through the membrane 18. Also, the temperature gradient in the reactor4 will be lower and thus the thermal stresses for the reactor 4 will decrease. This catalytic burner 20 can also be used to help control process conditions within the MCM reactor during start up or to address instabilities within the membrane/POXreactor 4 associated with the autothermal reforming and potential catalyst deactivation. The temperature of the MCM reactor will be very sensitive to the amount of O.sub.2 present and there could be some strange transients during start up. A quickreacting catalytic burner 4 running on H.sub.2 could help for process control.
After the syngas 17.sub.1 has been cooled down in the low temperature heat exchanger 19, the syngas 17.sub.1 is then further cooled down in a CO shift reactor 22, lowering the temperature further to about 200-300.degree. C. Depending on thechosen cooling temperature, water will condense out or not. Since a low temperature favors the CO shift reaction it might be wise to keep the temperature low. This will also lower the water consumption for the cycle since the condensed water 23 can bere-injected in the bottoming steam cycle 11. The medium used for the cooling is boiler feed water 24.sub.1, 24.sub.2 from a bottoming steam and water cycle 11. During the cooling of the syngas 17.sub.1, in the CO shift reactor 22, the syngas 17.sub.1undergoes the following reaction: CO+H.sub.2OH.sub.2+CO.sub.2+41.15 kJ/mol
The CO shift reactor 22 is in other words used to convert CO and water to CO.sub.2 and more hydrogen. Also this reaction is mildly exothermic, leading to some of the water which was condensed out during the cooling (or all water if the coolingtemperature is high) being evaporated again, taking heat from the exothermic process described above. After the CO shift reactor 22 the syngas 17.sub.2 consists ideally of H.sub.2, CO.sub.2 and H.sub.2O. This syngas 17.sub.2 is then lead to some kindof CO.sub.2 absorption equipment 25, based on either chemical or physical absorption. The CO.sub.2 removal rate in this kind of equipment is around 90%. Low pressure steam 26 needed for the CO.sub.2 removal is extracted from the steam turbine 12, andthe condensed water 27 is lead back to the feed water tank of the steam cycle 11. The removed CO.sub.2 28 is further compressed by means of inter-cooling in a compressor 29, producing liquid CO.sub.2 30 that might be deposited or used in for instanceenhanced oil recovery.
After removing most of the CO.sub.2, the syngas 17.sub.3 mainly consisting of H.sub.2, H.sub.2O and some remaining CO.sub.2 is lead to a combustion chamber 5, to be burned together with air from the first side of the membrane/POX reactor 4. Thewater in the syngas 17.sub.3 helps control the combustion temperature and thus lowers NO.sub.x formation. A part of the resulting syngas 17.sub.3 comprising hydrogen 6 from the CO.sub.2 removal equipment 25 can as well be burned in the catalytic burner20.
LIST OF DESIGNATIONS
1 Air 2 Compressor 3 Compressed air 4 Membrane/partial oxidation (POX) reactor 5 Combustion chamber 6 Hydrogen 7 Gas turbine 8 Generator 9 Hot flue gases 10 Heat recovery steam generator 11 Bottoming steam cycle 12 Steam Turbine 13 Generator 14Natural gas 15 Superheated steam 16 Medium temperature heat exchanger 17.sub.1, 17.sub.2, 17.sub.3 Syngas 18 Membrane 19 Low temperature heat exchanger. 20 Catalytic burner 21 Hydrogen 22 CO shift reactor 23 Condensed water 24 Boiler feed water 25CO.sub.2 absorption equipment 26 Low pressure steam 27 Condensed water 28 CO.sub.2 29 compressor 30 liquid CO.sub.2
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